CN103542692A - 基于缠绕管式换热器的非常规天然气液化系统 - Google Patents

基于缠绕管式换热器的非常规天然气液化系统 Download PDF

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CN103542692A
CN103542692A CN201210236962.8A CN201210236962A CN103542692A CN 103542692 A CN103542692 A CN 103542692A CN 201210236962 A CN201210236962 A CN 201210236962A CN 103542692 A CN103542692 A CN 103542692A
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heat exchanger
azeotrope
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CN103542692B (zh
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唐令力
单彤文
陈杰
花亦怀
浦晖
邰晓亮
冯颉
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China National Offshore Oil Corp CNOOC
CNOOC Gas and Power Group Co Ltd
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Abstract

本发明公开了一种基于缠绕管式换热器的非常规天然气液化系统。该液化系统包括缠绕管式换热器、燃料气换热器、重烃换热器和混合冷剂循环机构；所述混合冷剂循环机构包括依次相连的一级混合冷剂压缩机和一级混合冷剂压缩机冷却器；燃料气换热器、重烃换热器和所述缠绕管式换热器的预冷段依次相连通，所述缠绕管式换热器的预冷段的出口与重烃分离器相连通；所述重烃分离器的合格组分出口与所述缠绕管式换热器的液化段相连通，该液化段的出口分别与低温精馏塔和所述缠绕管式换热器的过冷段相连通，该过冷段的出口与所述低温精馏塔相连通；所述低温精馏塔的底部与LNG储罐相连通。本发明的主换热器采用缠绕管式换热器，相对于板翅式换热器，具有结构牢固、流道不易堵塞、泄漏点少、允许大温差传热的优点。

Description

基于缠绕管式换热器的非常规天然气液化系统
技术领域
本发明涉及一种基于缠绕管式换热器的非常规天然气液化系统，属于煤制气和焦炉尾气等非常规天然气液化技术领域。
背景技术
目前，国内常见的混合冷剂循环制冷工艺多基于板翅式换热器，在以常规的天然气为原料气的液化工厂中得到很好的应用。随着煤制气、焦炉尾气等非常规天然气的快速发展，国内已有的混合冷剂循环制冷工艺应用于原料气组分变化较大，以及氮气、氢气、重烃等杂质含量较高的非常规天然气时，会带来换热性能不佳、能耗大等问题。
国际上将缠绕管式换热器应用于基本负荷型液化工程作为主换热器。相对于板翅式换热器，缠绕管式换热器具有流道不易堵塞、泄漏点少、允许大温差传热和大温变速率等特点，因此，应用缠绕管式换热器对非常规天然气进行液化能够具有较好的适用性。
发明内容
本发明的目的是提供一种操作方便、安全可靠，效率高、适应性强的非常规天然气液化系统，该液化系统针对煤制气、焦炉尾气等非常规天然气的气质特点，合理利用冷能，降低能耗。
本发明所提供的一种基于缠绕管式换热器的非常规天然气液化系统，包括缠绕管式换热器、燃料气换热器、重烃换热器和混合冷剂循环机构；
所述混合冷剂循环机构包括依次相连的一级混合冷剂压缩机和一级混合冷剂压缩机冷却器；所述一级混合冷剂压缩机冷却器的出口与一混合冷剂气液分离器a相连通；所述混合冷剂气液分离器a的液相出口与所述缠绕管式换热器的预冷段相连通，该预冷段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；所述混合冷剂气液分离器a的气相出口与所述缠绕管式换热器的预冷段相连通，该预冷段的出口与混合冷剂气液分离器b相连通；所述混合冷剂气液分离器b的液相出口与所述缠绕管式换热器的液化段相连通，该液化段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；所述混合冷剂气液分离器b的气相出口依次与所述缠绕管式换热器的液化段和过冷段相连通，该过冷段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；
所述燃料气换热器、重烃换热器和所述缠绕管式换热器的预冷段依次相连通，所述缠绕管式换热器的预冷段的出口与重烃分离器相连通；所述重烃分离器的合格组分出口与所述缠绕管式换热器的液化段相连通，该液化段的出口分别与低温精馏塔和所述缠绕管式换热器的过冷段相连通，该过冷段的出口与所述低温精馏塔相连通，所述缠绕管式换热器的液化段出口和过冷段出口与所述低温精馏塔之间的管路上均设有节流阀；所述低温精馏塔的底部与LNG储罐相连通。
上述的非常规天然气液化系统中，所述混合冷剂循环机构还可包括依次与所述一级混合冷剂压缩机冷却器相连接的二级混合冷剂压缩机和二级混合冷剂压缩机冷却器。
上述的非常规天然气液化系统中，所述混合冷剂循环机构还可进一步包括依次与所述二级混合冷剂压缩机冷却器相连接的三级混合冷剂压缩机和三级混合冷剂压缩机冷却器。
上述的非常规天然气液化系统中，所述节流阀具体可为J/T阀。
上述的非常规天然气液化系统中，所述重烃分离器的重烃组分出口与所述重烃换热器相连通，用来对一股原料气进行冷却。
上述的非常规天然气液化系统中，所述低温精馏塔的顶部出口与所述燃料气换热器相连通，用来冷却一股原料气。
上述的非常规天然气液化系统中，所述低温精馏塔与所述LNG储罐之间设有LNG泵。
上述的非常规天然气液化系统中，所述一级混合冷剂压缩机、二级混合冷剂压缩机和/或三级混合冷剂压缩机均可为离心式压缩机。
本发明提供的液化系统主要适用于单列装置LNG产量在100万吨/年以下的中小型非常规天然气液化工厂。该液化系统将经过脱酸、脱水处理合格后的非常规天然气引入缠绕管式换热器，在缠绕管式换热器内经过预冷后将C2+的重烃脱除，再次进入缠绕管式换热器进行液化，一股流体进入脱除塔，与经过过冷后的LNG进行接触，脱除LNG中的氢、氮等杂质，脱除杂质合格后的LNG进入储罐。缠绕管式换热器所需冷量由混合冷剂压缩机提供。
与现有技术相比，本发明具有如下优点：第一，主换热器采用缠绕管式换热器，相对于板翅式换热器，具有结构牢固、流道不易堵塞、泄漏点少、允许大温差传热的优点；第二，本发明不仅适用于常规天然气，也可处理富含氢、氮的非常规天然气；第三，本发明进行天然气液化的效率较高，操作弹性较大。
附图说明
图1为本发明提供的非常规天然气液化系统的结构示意图。
图中各标记如下：1缠绕管式换热器、2燃料气换热器、3重烃换热器、41一级混合冷剂压缩机、42二级混合冷剂压缩机、51一级混合冷剂压缩机冷却器、52二级混合冷剂压缩机冷却器、61混合冷剂气液分离器a、62混合冷剂气液分离器b、71，72，73J/T阀、8重烃分离器、9低温精馏塔、10LNG储罐、11LNG泵。
具体实施方式
下面结合附图对发明做进一步说明，但本发明并不局限于以下实施例。
如图1所示，本发明提供的基于缠绕管式换热器的非常规天然气液化系统包括缠绕管式换热器1、燃料气换热器2、重烃换热器3和混合冷剂循环机构；该混合冷剂循环机构包括依次相连的一级混合冷剂压缩机41、一级混合冷剂压缩机冷却器51、二级混合冷剂压缩机42和二级混合冷剂压缩机冷却器52，一级混合冷剂压缩机41和二级混合冷剂压缩机42均为离心式压缩机；该二级混合冷剂压缩机冷却器52的出口与一混合冷剂气液分离器a61相连通；该混合冷剂气液分离器a61的液相出口与缠绕管式换热器1的预冷段相连通，该预冷段的出口与缠绕管式换热器1的壳侧相连通，该连通处设有J/T阀71；该混合冷剂气液分离器a61的气相出口与缠绕管式换热器1的预冷段相连通，该预冷段的出口与混合冷剂气液分离器b62相连通；其中混合冷剂气液分离器b62的液相出口与缠绕管式换热器1的液化段相连通，该液化段的出口与缠绕管式换热器1的壳侧相连通，该连通处设有J/T阀72；其中混合冷剂气液分离器b62的气相出口依次与缠绕管式换热器1的液化段和过冷段相连通，该过冷段的出口与缠绕管式换热器1的壳侧相连通，该连通处设有J/T阀73；燃料气换热器2、重烃换热器3和缠绕管式换热器1的预冷段依次相连通，其中缠绕管式换热器1的预冷段的出口与重烃分离器8相连通；
该重烃分离器8的重烃组分出口与重烃换热器3相连通，用于对一股原料气进行冷却，该重烃分离器8的合格组分出口与缠绕管式换热器1的液化段相连通，该液化段的出口分别与低温精馏塔9和缠绕管式换热器1的过冷段相连通，该过冷段的出口又与低温精馏塔9相连通，其中缠绕管式换热器1的液化段出口和过冷段出口与低温精馏塔9之间的管路上分别设有J/T阀74和75；低温精馏塔9的底部与LNG储罐10相连通，该连通的管路上设有LNG泵11，则脱除杂质合格后的LNG进入LNG储罐10，低温精馏塔9的顶部出口与燃料气换热器2相连通，则得到富含氮气、氢气及甲烷的燃料气。
使用本发明提供的液化系统对某焦炉尾气（原料气）进行液化，原料气摩尔组成为60.11%甲烷、4.38%乙烷、1.73%丙烷、1.76%丁烷、2.64%异丁烷、3.06%C5+、17.53%氮气和8.79%氢气；采用的混合冷剂的组分为26.9%甲烷、34.6%乙烯、15.4%丙烷、15.3%异戊烷和7.8%氮气。
主要实施步骤如下：
温度为45.0℃、压力为5.0MPaA的原料气进入缠绕管式换热器1预冷段进行预冷，与经过燃料气换热器2和重烃换热器3换热后的另一股原料气汇合，再次输送至预冷段并降温到-38.0℃后进入重烃分离器8，在重烃分离器8中将原料气中C2+分离出来并输送至重烃换热器3，用来对一股原料气进行冷却。脱除重烃后的原料气输送至缠绕管式换热器1液化段继续降温，当温度降低至-85.0℃时抽出一股LNG经J/T阀74节流降压至0.125MPaA后进入低温精馏塔9，另一股原料气继续液化并过冷至-155.0℃，经J/T阀75节流降压至0.116MPaA后从缠绕管式换热器1顶部流出进入低温精馏塔9中，在低温精馏塔9内两股流体进行接触换热并脱除LNG中的氮气、氢气等杂质，富含氮气、氢气及甲烷的燃料气从低温精馏塔9的上部流出，进入燃料气换热器2用来冷却一股原料气；合格的LNG从低温精馏塔9的底部流出进入LNG储罐10。
来自缠绕管式换热器1的低压混合冷剂温度约为40.1℃、压力为0.37MPaA，依次经一级混合冷剂压缩机41和二级混合冷剂压缩机42压缩至4.05MPaA。压缩后的高压高温气相混合冷剂经二级混合冷剂压缩机冷却器52冷却至45.0℃后，经过混合冷剂气液分离器a61后分别进入缠绕管式换热器1预冷段，液相冷剂被冷却至-38.0℃后，经J/T阀71节流降压至0.38MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量；被冷却的气相冷剂经过混合冷剂气液分离器b62分离后，气相和液相分别进入缠绕管式换热器1的液化段，液相冷剂被冷却至-85.0℃后，经J/T阀72节流降压至0.39MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量；被冷却的气相冷剂继续进入过冷段冷却至-155.0℃后，经J/T阀73节流降压至0.41MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量，最终换热后的气相混合冷剂进入一级混合冷剂压缩机41压缩入口，完成一个循环。
对原料气组分进行调整，使其重组分增多，原料气摩尔组分为：55.32%甲烷、7.38%乙烷、2.12%丙烷、1.86%丁烷、2.95%异丁烷、3.36%C5+、18.14%氮气和8.87%氢气；使用上述的液化系统对该原料气进行液化，混合冷剂的组分为24.4%甲烷、32.1%乙烯、16.1%丙烷、17.8%异戊烷和9.6%氮气，具体过程同上，经计算，甲烷液化率为85.04%。
使用上述提供的液化系统对某高含氮的管道天然气进行液化，其中原料气摩尔组分为：78.08%甲烷、0.83%乙烷、0.26%丙烷、0.11%丁烷、0.04%异丁烷、0.02%C5+和20.66%氮气；混合冷剂的组分为37.04%甲烷、23.91%乙烯、12.87%丙烷、19.79%异戊烷和6.39%氮气。
主要实施步骤如下：
温度为40.0℃、压力为3.5MPaA的原料气进入缠绕管式换热器1预冷段进行预冷，与经过燃料气换热器2和重烃换热器3换热后的另一股原料气汇合，再次输送至预冷段并降温到-38.0℃后进入重烃分离器8，在重烃分离器8中将原料气中C2+分离出来并输送至重烃换热器3，用来对一股原料气进行冷却。脱除重烃后的原料气输送至缠绕管式换热器1液化段继续降温，当温度降低至-88.0℃时抽出一股LNG经J/T阀74节流降压至0.11MPaA后进入低温精馏塔9，另一股原料气继续液化并过冷至-155.0℃，经J-T阀75节流降压至0.10MPaA后从缠绕管式换热器1顶部流出进入低温精馏塔9，在低温精馏塔9内两股流体进行接触换热并脱除LNG中的氮气，富含氮气及甲烷的燃料气从低温精馏塔9的上部流出，进入燃料气换热器2用来冷却一股原料气；合格的LNG从低温精馏塔9的底部流出进入LNG储罐10。
来自缠绕管式换热器1的低压混合冷剂温度约为36.0℃、压力为0.320MPaA，依次经一级混合冷剂压缩机41和二级混合冷剂压缩机42压缩至4.0MPaA。压缩后的高压高温气相混合冷剂首先经二级混合冷剂压缩机冷却器52冷却至40.0℃后，经过混合冷剂气液分离器a61后分别进入缠绕管式换热器1预冷段，液相冷剂被冷却至-38.0℃后，经J/T阀71节流降压至0.326MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量；被冷却的气相冷剂经过混合冷剂气液分离器b62分离后，气相和液相分别进入缠绕管式换热器1的液化段，液相冷剂被冷却至-85.0℃后，经J/T阀72节流降压至0.332MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量；被冷却的气相冷剂继续进入过冷段冷却至-155.0℃后，经J/T阀73节流降压至0.340MPaA后返回至缠绕管式换热器1壳侧为管侧流体提供冷量，最终换热后的气相混合冷剂进入一级混合冷剂压缩机41入口，完成一个循环。

Claims (8)

1.一种基于缠绕管式换热器的非常规天然气液化系统，其特征在于：该液化系统包括缠绕管式换热器、燃料气换热器、重烃换热器和混合冷剂循环机构；
所述混合冷剂循环机构包括依次相连的一级混合冷剂压缩机和一级混合冷剂压缩机冷却器；所述一级混合冷剂压缩机冷却器的出口与一混合冷剂气液分离器a相连通；所述混合冷剂气液分离器a的液相出口与所述缠绕管式换热器的预冷段相连通，该预冷段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；所述混合冷剂气液分离器a的气相出口与所述缠绕管式换热器的预冷段相连通，该预冷段的出口与混合冷剂气液分离器b相连通；所述混合冷剂气液分离器b的液相出口与所述缠绕管式换热器的液化段相连通，该液化段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；所述混合冷剂气液分离器b的气相出口依次与所述缠绕管式换热器的液化段和过冷段相连通，该过冷段的出口与所述缠绕管式换热器壳侧相连通，该连通处设有节流阀；
所述燃料气换热器、重烃换热器和所述缠绕管式换热器的预冷段依次相连通，所述缠绕管式换热器的预冷段的出口与重烃分离器相连通；所述重烃分离器的合格组分出口与所述缠绕管式换热器的液化段相连通，该液化段的出口分别与低温精馏塔和所述缠绕管式换热器的过冷段相连通，该过冷段的出口与所述低温精馏塔相连通，所述缠绕管式换热器的液化段出口和过冷段出口与所述低温精馏塔之间的管路上均设有节流阀；所述低温精馏塔的底部与LNG储罐相连通。
2.根据权利要求1所述的液化系统，其特征在于：所述混合冷剂循环机构还包括依次与所述一级混合冷剂压缩机冷却器相连接的二级混合冷剂压缩机和二级混合冷剂压缩机冷却器。
3.根据权利要求2所述的液化系统，其特征在于：所述混合冷剂循环机构还包括依次与所述二级混合冷剂压缩机冷却器相连接的三级混合冷剂压缩机和三级混合冷剂压缩机冷却器。
4.根据权利要求1-3中任一所述的液化系统，其特征在于：所述节流阀为J/T阀。
5.根据权利要求1-4中任一所述的液化系统，其特征在于：所述重烃分离器的重烃组分出口与所述重烃换热器相连通。
6.根据权利要求1-5中任一所述的液化系统，其特征在于：所述低温精馏塔的顶部出口与所述燃料气换热器相连通。
7.根据权利要求1-6中任一所述的液化系统，其特征在于：所述低温精馏塔与所述LNG储罐之间设有LNG泵。
8.根据权利要求1-7中任一所述的液化系统，其特征在于：所述一级混合冷剂压缩机、二级混合冷剂压缩机和/或三级混合冷剂压缩机为离心式压缩机。
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CN110749159B (zh) * 2019-10-22 2021-05-11 中海石油气电集团有限责任公司 一种天然气制冷液化的装置及方法
CN114413573A (zh) * 2022-01-20 2022-04-29 四川空分设备(集团)有限责任公司 基于绕管式换热器的天然气液化系统及工艺
CN114413573B (zh) * 2022-01-20 2023-11-17 四川空分设备(集团)有限责任公司 基于绕管式换热器的天然气液化系统及工艺
CN115371355A (zh) * 2022-08-16 2022-11-22 中海石油气电集团有限责任公司 一种适用于标准模块化的天然气液化系统及方法
CN115371355B (zh) * 2022-08-16 2023-10-20 中海石油气电集团有限责任公司 一种适用于标准模块化的天然气液化系统及方法

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